EP1873469A2 - Système pour augmenter la capacité d'un liquéfacteur à base de GNL dans un procédé de séparation d'air - Google Patents

Système pour augmenter la capacité d'un liquéfacteur à base de GNL dans un procédé de séparation d'air Download PDF

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Publication number
EP1873469A2
EP1873469A2 EP07111391A EP07111391A EP1873469A2 EP 1873469 A2 EP1873469 A2 EP 1873469A2 EP 07111391 A EP07111391 A EP 07111391A EP 07111391 A EP07111391 A EP 07111391A EP 1873469 A2 EP1873469 A2 EP 1873469A2
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EP
European Patent Office
Prior art keywords
nitrogen
stream
lng
pressure
column
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP07111391A
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German (de)
English (en)
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EP1873469A3 (fr
Inventor
Douglas Paul Dee
Jung Soo Choe
Donn Michael Herron
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Publication date
Application filed by Air Products and Chemicals Inc filed Critical Air Products and Chemicals Inc
Publication of EP1873469A2 publication Critical patent/EP1873469A2/fr
Publication of EP1873469A3 publication Critical patent/EP1873469A3/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—Nitrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0244—Operation; Control and regulation; Instrumentation
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
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    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Definitions

  • the present invention concerns the known embodiment of the above-described Process wherein, in order to provide the refrigeration necessary when at least a portion of the product is desired as liquid, refrigeration is extracted from liquefied natural gas (hereafter "LNG”) by feeding nitrogen from the distillation column system to an insulated liquefier unit (hereafter “LNG-based liquefier”) where it is liquefied. If at least a portion of the liquid product desired is liquid oxygen, at least a portion of the liquefied nitrogen is returned to the distillation column system (or optionally the main heat exchanger). Otherwise, the liquefied nitrogen is withdrawn as product.
  • LNG liquefied natural gas
  • LNG-based liquefier insulated liquefier unit
  • An LNG-based liquefier is typically oversized to accommodate a projected increase in demand of liquid products after the initial years of operation. This is particularly true for liquid nitrogen since the demand for liquid nitrogen out of any particularly ASU often grows faster than the demand for liquid oxygen above the base load of liquid oxygen for which the plant is designed. A problem with this oversizing approach however is the incremental capital cost incurred does not begin to pay off until the projected demand increase is actually realized (if at all). Furthermore, capital costs are particularly sensitive for LNG-based liquefiers since, as opposed to conventional liquefiers which are typically located near the customers of the liquid products, LNG-based liquefiers must be located near an LNG receiving terminal and thus incur a product transportation cost penalty.
  • the capacity of an LNG-based liquefier can be increased by adding a dense fluid expander. However, only modest capacity increases can be achieved in this manner.
  • the LNG is not sufficiently cold to liquefy a low-pressure nitrogen gas.
  • the boiling temperature would be typically above -260°F (-162°C), and the nitrogen would need to be compressed to at least 15.5 bara (1.55 MPa) in order to condense.
  • the LNG vaporization pressure is increased, so too will the required nitrogen pressure be increased. Therefore, multiple stages of nitrogen compression are required, and LNG can be used to provide cooling for the compressor intercooler and aftercooler.
  • EP-A-0,304,355 (hereafter "EP '355") teaches the use of an inert gas recycle such as nitrogen or argon to act as a medium to transfer refrigeration from the LNG to the air separation plant.
  • the high pressure inert gas stream is liquefied against vaporizing LNG then used to cool medium pressure streams from the air separation unit (ASU).
  • ASU air separation unit
  • One of the ASU streams, after cooling, is cold compressed, liquefied and returned to the ASU as refrigerant.
  • the motivation here is to maintain the streams in the same heat exchanger as the LNG at a higher pressure than the LNG. This is done to assure that LNG cannot leak into the nitrogen streams, i.e. to ensure that methane cannot be transported into the ASU with the liquefied return nitrogen.
  • the authors also assert that the bulk of the refrigeration needed for the ASU is blown as reflux liquid into a rectifying column.
  • the low pressure nitrogen Prior to boosting the pressure of the low pressure nitrogen, the low pressure nitrogen may be combined with a gaseous nitrogen vent stream from the LNG-based liquefier and, after boosting the pressure of the low pressure nitrogen but before feeding it to the LNG-based liquefier, the low pressure nitrogen may be cooled by indirect heat exchange against a cooling medium in a supplemental aftercooling heat exchanger that is separate and distinct from the auxiliary heat exchanger.
  • an apparatus for the cryogenic separation of air comprising:
  • the system may comprise a supplemental aftercooling heat exchanger that is separate and distinct from the auxiliary heat exchanger for cooling LP nitrogen by indirect heat exchange against a cooling medium.
  • Stream 182 is ultimately rejected to the atmosphere.
  • Stream 176 is processed in the LNG-based liquefier 2 to create liquefied nitrogen product stream 188 and liquid nitrogen refrigerant stream 186.
  • Liquid nitrogen refrigerant stream 186 is introduced into the distillation columns through valves 136 and 140.
  • Refrigeration for LNG-based liquefier is provided from LNG stream 194, which is vaporized and heated to produce stream 198.
  • the only nitrogen feed to the LNG-based liquefier is stream 176, which originates from the higher pressure column 114.
  • Stream 182 is transformed utilizing a supplemental compressor and the associated heat exchange equipment (referred to hereunder as the "supplemental processing unit" which is depicted as unit 3 in Figure 1 a) to become stream 184, then mixed with stream 176, to form a feed to the LNG-based liquefier 2.
  • supplemental processing unit which is depicted as unit 3 in Figure 1 a
  • Liquefied nitrogen product stream 188 and liquid nitrogen refrigerant stream 186 are produced within the LNG-based liquefier.
  • Liquid nitrogen refrigerant stream 186 is introduced into the distillation columns through valves 136 and 140.
  • the source of the nitrogen feed to the LNG-based liquefier leaves the ASU as two streams, 182 and 176.
  • the supplemental processing unit as depicted as unit 3 in Figures 3b and 3c does not necessarily refer to single physical unit.
  • the supplemental compressor can be contained in a housing with other compressors while the supplemental heat exchanger can be contained in a housing with other heat exchangers.
  • the supplemental compressor and heat exchanger operate at above ambient temperature in Figure 3c's embodiment of the present invention, this equipment operates at below ambient temperatures in Figure 3b's embodiment and therefore must be insulated.
  • atmospheric air 100 is compressed in the main air compressor 102, purified in adsorbent bed 104 to remove impurities such as carbon dioxide and water, then divided into two fractions: stream 230 and stream 208.
  • Stream 208 is cooled in main heat exchanger 110 to become stream 212, the vapor feed air to the higher pressure column 114.
  • Stream 230 is cooled to a temperature near that of stream 212 then at least partially condensed to form stream 232, split into streams 434 and 438, then eventually reduced in pressure across valves 236 and 240 and introduced to the higher pressure column 114 and lower pressure column 116.
  • the higher pressure column produces a nitrogen-enriched vapor from the top, stream 462, and an oxygen-enriched stream, 450, from the bottom.
  • Stream 462 is split into stream 174 and stream 464.
  • Stream 174 is warmed in the main heat exchanger then passed, as stream 176 to the LNG-based liquefier 2.
  • Stream 464 is condensed in reboiler-condenser 418 to form stream 466.
  • a portion of stream 466 is returned to the higher pressure column as reflux (stream 468); the remainder, stream 470, is eventually introduced to the lower pressure column as the top feed to that column through valve 472.
  • Oxygen-enriched stream 450 is passed to the argon column's reboiler-condenser 484 through valve 452, and at least partially vaporized to form stream 456, which is directed to the lower pressure column.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP07111391A 2006-06-30 2007-06-29 Système pour augmenter la capacité d'un liquéfacteur à base de GNL dans un procédé de séparation d'air Withdrawn EP1873469A3 (fr)

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US11/477,924 US7712331B2 (en) 2006-06-30 2006-06-30 System to increase capacity of LNG-based liquefier in air separation process

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EP1873469A3 EP1873469A3 (fr) 2012-08-01

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US (1) US7712331B2 (fr)
EP (1) EP1873469A3 (fr)
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CN (1) CN101097112B (fr)
CA (1) CA2593649C (fr)
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TWI302188B (en) 2008-10-21
MX2007007878A (es) 2008-12-16
CN101097112A (zh) 2008-01-02
US7712331B2 (en) 2010-05-11
KR100874680B1 (ko) 2008-12-18
CA2593649C (fr) 2012-03-13
JP2008025986A (ja) 2008-02-07
KR20080002673A (ko) 2008-01-04
US20080000266A1 (en) 2008-01-03
EP1873469A3 (fr) 2012-08-01
SG138574A1 (en) 2008-01-28
CN101097112B (zh) 2012-09-19
JP5015674B2 (ja) 2012-08-29
CA2593649A1 (fr) 2007-12-30

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